GB2121430A - Olefin isomerisation process - Google Patents
Olefin isomerisation process Download PDFInfo
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- GB2121430A GB2121430A GB08313561A GB8313561A GB2121430A GB 2121430 A GB2121430 A GB 2121430A GB 08313561 A GB08313561 A GB 08313561A GB 8313561 A GB8313561 A GB 8313561A GB 2121430 A GB2121430 A GB 2121430A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/23—Rearrangement of carbon-to-carbon unsaturated bonds
- C07C5/25—Migration of carbon-to-carbon double bonds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/22—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by isomerisation
- C07C5/23—Rearrangement of carbon-to-carbon unsaturated bonds
- C07C5/25—Migration of carbon-to-carbon double bonds
- C07C5/2506—Catalytic processes
- C07C5/2512—Catalytic processes with metal oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/02—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the alkali- or alkaline earth metals or beryllium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/08—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of gallium, indium or thallium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
- B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
- B01J23/74—Iron group metals
Description
k 1
SPECIFICATION Olefin isomerisation process
GB 2 121 430 A 1 This invention relates to an olefin isomerisation process. More particularly, the invention relates to a process for the isomerisation of butene-2 to butene-1.
Certain olefin isomerisation processes are known, and reference can be made in this respect to 5 US-A-347551 1 and US-A-422961 0.
The processes of the known art have not however found any industrial application, in that the catalysts used in them are difficult to regenerate due to the formation of carbon residues during operation. Regeneration must be effected at high temperature, and the known catalysts lose their activity characteristics during this, mainly because of the collapse of the surface area. In the Journal of 10 Catalysis, 49, 285, (1977) it is stated that butene isomerisation can be effected in the presence of a catalyst constituted by lanthanum oxides. The tests reported therein show however that the reaction is very slow, with the result that very low space velocities are necessary in order to attain acceptable conversion, and in addition the catalyst is sensitive even to traces of moisture, so that it has to be regenerated in a very complicated and costly manner.
It has been surprisingly found that the drawbacks of the known art can be obviated by using for the olefin isomerisation reaction a catalyst comprising in its final form, A12SO.3. SiO,, and an oxide of one or more bivalent or trivalent metals chosen from those of Group 2a (particularly calcium, barium or strontium), and/or Group 8 (particularly iron), and/or Group 3b (particularly lanthanum) and/or the lanthanides.
The Periodic Table referred to herein is that published in "Handbook of Chemistry and Physics", 55th edition, edited by Robert C. Weast and published by CRC Press, Ohio.
The process according to the present invention comprises bringing the olefin to be isomerised into contact, preferably at a temperature of from 350 to 55WIC (more preferably from 450 to 500IC) and preferably at a pressure of from 0. 1 to 10 atmospheres (more preferably from 0.5 to 3 atmospheres, 25 with a gamma alumina-based catalyst having the general molar formula:
aAl20.. bS'02.cMe.0y wherein Me.O. is the oxide of the bivalent or trivalent metal or metals chosen as above, and a, b and c respectively, b and c being related by the are the number of moles of A12S01, S'02 and Me,,0, relationship C > mb + B, wherein B has a value greater than or equal to 0. 01, and b has a value 30 between 0 (in which event the catalyst does not contain S'02) and 0.300, preferably between 0.020 and 0.250, the ratio (b + c):a being between 0.01:1 and 9.0:1, and m being a number between 0.7 and 0.1.
In the specific case of lanthanum, it has been found that the optimum relationship between the lanthanum oxide and the silica is as follows:
moles La20, > 0.257 (moles S'02) + 0.014 whereas in the case of calcium, the optimum relationship between the calcium oxide and the silica is as follows:
moles CaO >, 0.500 (moles Si02) + 0.030.
In the case of barium the optimum relationship between the barium oxide and the silica is as 40 follows:
moles BaO > 0.500 (moles SiO,) + 0.020.
In the case of iron the optimum relationship between the ferric oxide and the silica is as follows:
moles Fe203 > 0.29 (moles S'02) + 0.018.
According to the process of the present invention, the weight hourly space velocity (WHSV) of the 45 olefin is preferably from 2 to 20 h-', more preferably from 4 to 8 h.
Regeneration may be effected in the conventional manner by heating in a controlled oxygen atmosphere to a temperature of from 470 to 6001C.
The catalyst for use according to the invention may be prepared by the following two stages:
(a) preparation of gamma alumina stabilised by silica, the stabilisation preferably being carried out 50 by a method as described in US-E-30668, US-A-4013590 or US-A-4015589; (b) impregnation of the alumina stabilised as in (a) with a salt of one or more of said bivalent or trivalent metals, preferably a nitrate or acetate, followed by thermal treatment at a preferred temperature of from 350 to 5001C.
In an alternative procedure, normal gamma alumina, not stabilised by silica, is used, this alumina 55 being impregnated and treated as described in (b).
2 GB 2 121 430 A 2 It should be noted that the process according to the present invention not only enables the aforesaid regeneration drawbacks to be overcome, but also enables the level of isobutene produced when converting butene-2 to butene-1 to be maintained within the maximum allowable limits for the direct use of butene-1 in polymerisation reactions, i.e. without having to purify the butene-1.
Some of the catalysts used in the present invention is described and claimed in the British patent 5 application filed by us on the same day as the present application and claiming priority from Italian Patent Application No. 21512 A/82.
The invention will now be illustrated by the following Examples.
EXAMPLE 1
20 9 of gamma alumina (surface area 200 m/g) are impregnated with 15 cc of an aqueous 10 solution containing 1.8 g of lanthanum nitrate. It is dried and calcined at 5001C for 4 hours. A material is obtained comprising 3.5% by weight of La203 on alumina.
The catalyst obtained in this manner is placed in a flow reactor, in which the trans butene-2 isomerisation reaction is carried out. Table 1 gives the data relative to the test carried out, and the value of the surface areas of the materials concerned, after thermal treatment for 24 hours at 1 OOOOC. 15 EXAM P LE 2 Following the.procedure of Example 1, 20 g of alumina are impregnated with 15 cc of an aqueous solution containing 2.57 g of lanthanum nitrate.
A catalyst is obtained containing 5% by weight of La203 on alumina.
EXAMPLE 3 - Following the procedure of Example 1, a catalyst is prepared containing 7.5% by weight of La203 on alumina.
EXAMPLE 4 on alumina.
Following the procedure of Example 1, a catalyst is prepared containing 10.0% by weight of La203 EXAMPLE 5 g of gamma alumina (S.A.a 200 m2/g) are treated with 15 cc of an alcohol solution containing 0.75 g of Dynasil A 40 (40% ethyl orthosilicate solution).
The mixture is allowed to react at 501C, it is then drained off and treated with steam in order to 30 hydrolyse the silanol groups. It is dried and calcined at 5001C for 4 hours.
The material thus obtained, containing 1.5% of S'02, is impregnated with 2.57 g of lanthanum nitrate, as described in Example 2.
A material is obtained constituted by gamma alumina stabilised by 1.5% of Si02, and containing 5% of La203'This catalyst is loaded into a reactor, in which the isomerisation of trans butene-2 is carried out.
Table 2 gives the data relative to the tests carried out, and the value of the surface areas bf the materials concerned, after thermal treatment for 24 hours at 1 0001C.
EXAMPLE 6
9 of silicified alumina, prepared as described in Example 5, are impregnated with an aqueous lanthanum nitrate solution by the procedure described in Example 3. A material is obtained consisting of 40 alumina and 1.5% SiO, plus 7.5% La203.
EXAMPLE 7 - A catalyst is prepared in the manner heretofore described, constituted by alumina, stabilised by 1.5% Si02 and modified by 10% of La103.
EXAMPLE 8 g of alumina are impregnated, by the procedure of Example 5, with an alcohol solution of ethyl orthosilicate to give a material which, after treatment with steam and calcining, contains 3.8% of Si02.
This material is then impregnated with the necessary quantity of lanthanum nitrate solution to give 5.0% of La20.. A catalyst is obtained in this manner containing 3.8% Si02 and 5.0% La20. on alumina.
Catalytic tests are carried out with this material.
EXAMPLE 9
A catalyst of composition 3.8% S'02 and 7.5% La203 on alumina is prepared in the manner described in Example 8.
3 EXAMPLE 10
GB 2 121 430 A 3 A catalyst of composition 3.8% S'02 and 10.0% La20. on alumina is prepared in the manner.
described in Example 8.
EXAMPLE 11
A catalyst of composition 8% SiO, ard 5% La,O, on alumina is prepared in the aforesaid manner.5 EXAMPLE 12 manner.
A catalyst of composition 8% S'02 end 7.5% La20. on alumina is prepared in the aforesaid EXAMPLE 13
1Q A catalyst of composition 8% S'02 and 10.0% La201 on alumina is prepared in the aforesaid 10 manner.
EXAMPLE 14.
EXAMPLE 22 manner.
A catalyst of composition 8% S'02 and 15.0% La203 on alumina is prepared in the aforesaid EXAMPLE 15
Using the silicified alumina prepared as described in Example 8, a catalyst is prepared by impregnating said silicified alumina (3.8% Si0J with an aqueous solution of rare earth acetate, in a quantity such as to provide a final catalyst containing 10% of rare earth oxide.
The data given in Table 2 show the extent to which the behaviour of pure lanthanum and a mixture of rare earths is identical.
EXAMPLE 16
A catalyst of composition 1.5% S'02 + 2.5% CaO on alumina is prepared in the aforesaid manner. The calcium is introduced, analogously to the lanthanum, by using a calcium nitrate solution.
The data are given in Table 3.
EXAMPLE 17
A cataiyst of composition 1.5% S'02 + 5.0% CaO on alumina is prepared.
EXAMPLE 13
A catalyst of composition 1.5% S'02 + 7.5% CaO on alumina isprepared.
EXAMPLE 19
A catalyst of composition 3.8% S'02 + 2.5% CaO on alumina is prepared.
EXAMPLE 20
A catalyst of composition 3.8% S'02 + 5.0% CaO on alumina is prepared.
EXAMPLE 21
A catalyst of composition 3.8% S'02 + 7.5% CaO on alumina is prepared.
A catalyst of composition 1.5% S'02 + 4.0% BaO on alumina is prepared in the aforesaid manner (the barium is introduced analogously to the calcium, by using a barium nitrate solution).
The data are given in Table 4.
EXAMPLE 23
A catalyst of composition 1.5% S'02 + 8.0% BaO on alumina is prepared.
EXAMPLE 24
A catalyst of composition 30 SiO, + 4.0% BaO on alumina is prepared in the aforesaid manner.
EXAMPLE 25
A catalyst of. composition 3.8% SiO, + 8.0% BaO on alumina is prepared in the aforesaid manner.
EXAMPLE 26 barium.
A catalyst of composition 3.3% SiO, + 3.5% SrO on alumina is prepared in the aforesaid manner. The results given in Table 4 show that strontium behaves in a manner analogous to calcium and 30.
4 GB 2 121 430 A 4 EXAMPLE 27
A catalyst of composition 1.5% S'02 and 2.5% Fe203 (by weight) on alumina is prepared in the aforesaid manner. (The iron is introduced as an aqueous solution of iron nitrate). The data are given in Table 5.
EXAMPLE 28 5
A catalyst of composition 1,5 S'02 and 3.8% Fe203 by weight on gamma alumina is prepared in the aforesaid manner.
EXAMPLE 29
A catalyst of composition 1.5% S'02 and 5.0% Fe203 on gamma alumina is prepared in the 10 aforesaid manner.
EXAMPLE 30
A catalyst of composition 3.8% S'02 and 2.5% Fe203 on gamma alumina is prepared in the aforesaid manner.
EXAMPLE 31
A catalyst of composition 3.8% S'02 and 3.8% Fe203 by weight is prepared in the aforesaid is manner.
EXAMPLE 32
A catalyst of composition 3.8% S'02 and 5.0% Fe203 by weight is prepared in the aforesaid manner.
EXAMPLE 33
A catalyst of composition 5.0% S'02 and 2.5% Fe203 on gamma alumina is prepared in the aforesaid manner.
EXAMPLE 34
A catalyst of composition 5.0% Si02 and 3.8% Fe203 on gamma alumina is prepared in the 25 aforesaid manner.
EXAMPLE 35 manner.
A catalyst of composition 5.0% S'02 and 5% Fe203 on gamma alumina is prepared in the aforesaid EXAMPLE 36
A catalyst of composition 5.0% S'02 and 7.5% Fe203 on gamma alumina is prepared in the 30 aforesaid manner.
TABLE 1
Selective isomerisation of trans butene-2 to butene-1 Reaction conditions: T = 470OC; P = 1 ata; WHSV = 6 lsobutene content of reaction products (the Surface area linear butenes are always present in a quantity (24 h, 1 OOOOC) corresponding to thermodynamic equilibrium at Catalyst % La20. M2/g the reaction temperature) Ex 1 3.5 152 1300 p.p.m.
Ex 2 5.0 151 450 p.p.m.
Ex 3 7.5 120 350 p.p.m.
Ex 4 10.0 117 350 p.p.m.
N.B. Example 1 clearly shows that on operating outside the range of the invention, butene-1 cannot be obtained with an isobutene content below the maximum allowable limit (0. 1 % by weight with respect to the butene-1) t It i J r GB 2 121 430 A 5 TABLE 2 lsomerisation of trans butene-2 to butene-1 Reaction conditions: T = 470OC; P = 1 ata; WHSV = 6 1 1 r Catalyst % La203 % Si02 Surface area lsobutene content of reaction products (24 h, 1 0OWC) (the linear butenes are always present M2/g in a quantity corresponding to thermodynamic equilibrium at the reaction temperature) Ex 5 5.0 1.5 154 990 P.P.M.
Ex 6 7.5 1.5 134 490 p.p.m.
Ex 7 10.0 1.5 113 140 p.p.m.
Ex 8 5.0 3.8 164 0.35% Ex 9 7.5 3.8 163 0.145% Ex 10 10.0 3.8 139 330 p.p.m.
Ex 11 5.0 8.0 188 0.7% Ex 12 7.5 8.0 170 1.4% Ex 13 10.0 8.0 155 1500 P.P.M.
Ex 14 15.0 8.0 145 200 p.p.m.
Ex 15 10.0 (as rare 3.8 143 380 p.p.m.
earth oxides).
For Examples 5, 8, 9, 11, 12, 13, see note relative to Example 1.
TABLE 3 lsomerisation of trans butene-2 to butene-1 Reaction conditions: T = 470IC; P = 1 ata; WHSV = 6 Catalyst % CaO % Si02 Surface area lsobutene content of reaction products (24 h, 1 OOOOC) (the linear butenes are always present in a M2/g quantity corresponding to thermodynamic equilibrium at the reaction temperature) Ex16 2.5 1.5 183 150 p.p.m.
Ex 17 5.0 1.5 147 270 p.p.m.
Ex 18 7.5 1.5 136 300 p.p.m.
Ex 19 2.5 3.8 185 450 p.p.m.
Ex 20 5.0 3.8 155 250 p.p.m.
Ex 21 7.5 3.8 150 150 p.p.m.
All catalysts of Examples 1 to 20 were subjected to ageing tests consisting of 40 reaction cycles (332 hours in total) and 40 regeneration cycles (152 hours in total), without showing loss of activity. Regeneration was effected at a temperature of 5401C.
6 GB 2 121 430 A 6 TABLE4 Isomerisation of trans butene-2 to butene-1 Reaction conditions: T = 470OC; P = 1 ata; WHSV = 6 Catalyst % BaO % si02 Surface area Isobutene content of reaction products (by weight) (by weight) (24 h, 1 OOOOC) (the linear butenes are always present in a M2/g quantity corresponding to thermodynamic equilibrium at the reaction temperature) Ex 22 4.0 1.5 192 260 p.p.m.
Ex 23 8.0 1.5 151 130 p.p.m.
Ex 24 4.0 3.8 189 470 p.p.m.
Ex 25 8.0 3.8 154 230 p.p.m.
Ex 26 3,5% (SrO) 3.8 185 280 p.p.m.
TABLE5 Isomerisation of trans butene-2 to butene-1 Reaction conditions: T = 470OC; P = 1 ata; WHSV = 6 Catalyst % Fe20. % Si02 Surface area lsobutene content of reaction products (byweight) (byweight) (24h,1000IC) (the linear butenes are always present in a quantity M2/g corresponding to thermodynamic equilibrium at the reaction temperature).
Ex 27 2.5 1.5 161 1100 P.P.M.
Ex 28 3.8 1.5 129 430 p.p.m.
Ex 29 5.0 1.5 130 200 P.P.M.
Ex 30 2.5 3.8 158 0.41% Ex 31 3.8 3.8 165 0.12% Ex 32 5.0 3.8 141 420 p.p.m.
Ex 33 2.5 5.0 190 1.2% Ex 34 3.8 5.0 170 0.9% Ex 35 5.0 5.0 155 1800 p.p.m.
Ex 36 7.5 5.0 150 350 p.p.m.
For Examples 27, 30, 31, 33,34, 35,-see note relative to Example 1.
Claims (15)
1 e C > mb + B Y 7 h GB 2 121 430 A 7 wherein B has a value greater than or equal to 0.01, b has a value of from 0 to 0.300, the ratio (b + cha is from 0.01:1 to 9.0:1, and m is a number of from 0.1 to 0.7.
2. A process according to claim 1, wherein the olefin is isomerised at a temperature of from 350 to 5500C.
3. A process according to claim 2, wherein the olefin is isomerised at a temperature of from 450 5 to 5000c.
4. A process according to any of claims 1 to 3, wherein the olefin is isomerised at a pressure of from 0. 1 to 10 atmospheres.
5. A process according to claim 4, wherein the olefin is isomerised at a pressure of from 0.5 to 3 atmospheres.
h-'.
6. A process according to any of claims 1 to 5, wherein the space velocity of the olefin is from 2 to
7. A process according to claim 6, wherein the space velocity of the olefin is from 4 to 8 h-'.
8. A process according to any of claims 1 to 7, wherein the metal Me is calcium, and wherein the number of moles of CaO is related to the number of moles of S102 by the relationship:
moles CaO >, 0.500 (moles Si02) + 0.030.
9. A process according to any of claims 1 to 7, wherein the metal Me is barium, and wherein the number of moles of BaO is related to the number of moles of SiO, by the relationship:
moles BaO >, 0.500 (moles Si0J + 0.020.
10. A process according to any of claims 1 to 7, wherein the metal Me is lanthanum or a 20 lanthanide, and wherein the number of moles of La 203 or lanthanide oxide is related to the number of moles of S102 by the relationship:
moles La20. or lanthanide oxide > 0.257 (moles Si02) + 0.014.
11. A process according to any of claims 1 to 7, wherein the metal Me is iron, and wherein the number of moles of Fe203 is related to the number of moles of SiO2 by the relationship:
moles Fe 201 >, 0.290 (moles S'02) + 0.018.
12. A process according to any of claims 1 to 11, wherein the number of moles of S'02 is from 0.020 to 0.250.
13. A process according to any of claims 1 to 7, wherein the catalyst is substantially as described 30 in any of the foregoing Examples 1 to 36.
14. A process according to any of claims 1 to 13, wherein the olefin is butene-2 (which is isomerised to butene-1).
15. An isomerised olefin obtained by a process according to any of claims 1 to 14.
Printed for Her Majesty's Stationery Office by the Courier Press. Leamington Spa, 1983. Published by the Patent Office, 25 Southampton Buildings, London, WC2A lAY, from which copies may be obtained.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IT21511/82A IT1190839B (en) | 1982-05-27 | 1982-05-27 | PROCEDURE FOR THE ISOMERIZATION OF BOND OF THE OLEFINS |
Publications (3)
| Publication Number | Publication Date |
|---|---|
| GB8313561D0 GB8313561D0 (en) | 1983-06-22 |
| GB2121430A true GB2121430A (en) | 1983-12-21 |
| GB2121430B GB2121430B (en) | 1986-09-24 |
Family
ID=11182885
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| GB08313561A Expired GB2121430B (en) | 1982-05-27 | 1983-05-17 | Olefin isomerisation process |
Country Status (33)
| Country | Link |
|---|---|
| US (1) | US4814542A (en) |
| JP (1) | JPS58219128A (en) |
| KR (1) | KR870000055B1 (en) |
| AT (1) | AT382864B (en) |
| AU (1) | AU552806B2 (en) |
| BE (1) | BE896849A (en) |
| CA (1) | CA1199041A (en) |
| CS (1) | CS244933B2 (en) |
| DD (1) | DD209801A5 (en) |
| DE (1) | DE3319171A1 (en) |
| DK (1) | DK234583A (en) |
| ES (1) | ES8500201A1 (en) |
| FR (1) | FR2527596A1 (en) |
| GB (1) | GB2121430B (en) |
| GR (1) | GR81339B (en) |
| HU (1) | HUT34419A (en) |
| IN (2) | IN158661B (en) |
| IT (1) | IT1190839B (en) |
| LU (1) | LU84823A1 (en) |
| MW (1) | MW2283A1 (en) |
| NL (1) | NL8301872A (en) |
| NO (1) | NO831847L (en) |
| NZ (1) | NZ204340A (en) |
| PH (1) | PH17965A (en) |
| PL (1) | PL141424B1 (en) |
| PT (1) | PT76764B (en) |
| RO (1) | RO86409B (en) |
| SE (1) | SE8302849L (en) |
| SU (1) | SU1333231A3 (en) |
| YU (1) | YU113083A (en) |
| ZA (1) | ZA833396B (en) |
| ZM (1) | ZM3683A1 (en) |
| ZW (1) | ZW11283A1 (en) |
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|---|---|---|---|---|
| US4814542A (en) * | 1982-05-27 | 1989-03-21 | Snamprogetti, S.P.A. | Olefin bond isomerization process |
| US4841061A (en) * | 1985-12-27 | 1989-06-20 | Nippon Shokubai Kagaku Kogyo Co., Ltd. | Process for producing cyclic amines |
| US4841060A (en) * | 1985-12-23 | 1989-06-20 | Nippon Shokubai Kagaku Kogyo Co., Ltd. | Vapor-phase intramolecular dehydration reaction of alkanolamines |
| US5507940A (en) * | 1991-08-30 | 1996-04-16 | Shell Oil Company | Hydrodenitrification catalyst and process |
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| EP0225407A1 (en) * | 1985-01-25 | 1987-06-16 | Council of Scientific and Industrial Research | Lanthanum silicate materials, their production and use |
| FR2584388B1 (en) * | 1985-07-03 | 1991-02-15 | Rhone Poulenc Spec Chim | COMPOSITION BASED ON CERIC OXIDE, ITS PREPARATION AND USES THEREOF |
| DE4445680A1 (en) * | 1994-12-21 | 1996-06-27 | Huels Chemische Werke Ag | Catalyst and process for the isomerization of aliphatic C¶4¶-C¶1¶¶¶ monoolefins |
| US6875901B2 (en) * | 2001-05-23 | 2005-04-05 | Abb Lummus Global Inc. | Olefin isomerization process |
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| DE10311139A1 (en) | 2003-03-14 | 2004-09-23 | Basf Ag | Process for the production of 1-butene |
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| DE102008036295A1 (en) * | 2008-08-04 | 2010-02-11 | Bayer Technology Services Gmbh | Catalyst composition for transesterification |
| US8586813B2 (en) * | 2009-07-21 | 2013-11-19 | Lummus Technology Inc. | Catalyst for metathesis of ethylene and 2-butene and/or double bond isomerization |
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| JP6736017B2 (en) * | 2015-11-05 | 2020-08-05 | Ｅｎｅｏｓ株式会社 | Isomerization catalyst, method for producing linear olefin and method for producing compound |
| RU2722665C1 (en) * | 2016-07-28 | 2020-06-02 | Лионделл Кемикал Текнолоджи, Л.П. | Removal of paraffin from streams containing c4 |
| US10550048B2 (en) * | 2017-01-20 | 2020-02-04 | Saudi Arabian Oil Company | Multiple-stage catalyst system for self-metathesis with controlled isomerization and cracking |
| JP2020097544A (en) * | 2018-12-18 | 2020-06-25 | Ｊｘｔｇエネルギー株式会社 | Manufacturing method of straight chain monoolefin and manufacturing method of compound |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1267719A (en) * | 1969-12-05 | 1972-03-22 | Exxon Research Engineering Co | Isomerization of olefins |
| EP0066485A1 (en) * | 1981-05-21 | 1982-12-08 | Institut Français du Pétrole | Process for the isomerisation of olefines |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3313858A (en) * | 1965-02-12 | 1967-04-11 | Phillips Petroleum Co | Isomerization of non-terminal olefins |
| US3467727A (en) * | 1966-10-10 | 1969-09-16 | Universal Oil Prod Co | Isomerization of 2,3-dimethylbutenes |
| US3479415A (en) * | 1967-05-12 | 1969-11-18 | Air Prod & Chem | Isomerization of olefinic hydrocarbons |
| US3864424A (en) * | 1973-04-30 | 1975-02-04 | Universal Oil Prod Co | Isomerization process |
| US4217244A (en) * | 1978-05-11 | 1980-08-12 | Phillips Petroleum Company | Regeneration of isomerization catalysts containing magnesium oxide |
| US4229610A (en) * | 1978-11-03 | 1980-10-21 | Phillips Petroleum Company | Olefin double bond isomerization |
| IT1190839B (en) * | 1982-05-27 | 1988-02-24 | Anic Spa | PROCEDURE FOR THE ISOMERIZATION OF BOND OF THE OLEFINS |
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1982
- 1982-05-27 IT IT21511/82A patent/IT1190839B/en active
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1267719A (en) * | 1969-12-05 | 1972-03-22 | Exxon Research Engineering Co | Isomerization of olefins |
| EP0066485A1 (en) * | 1981-05-21 | 1982-12-08 | Institut Français du Pétrole | Process for the isomerisation of olefines |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4814542A (en) * | 1982-05-27 | 1989-03-21 | Snamprogetti, S.P.A. | Olefin bond isomerization process |
| US4841060A (en) * | 1985-12-23 | 1989-06-20 | Nippon Shokubai Kagaku Kogyo Co., Ltd. | Vapor-phase intramolecular dehydration reaction of alkanolamines |
| US4841061A (en) * | 1985-12-27 | 1989-06-20 | Nippon Shokubai Kagaku Kogyo Co., Ltd. | Process for producing cyclic amines |
| US5507940A (en) * | 1991-08-30 | 1996-04-16 | Shell Oil Company | Hydrodenitrification catalyst and process |
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| PCNP | Patent ceased through non-payment of renewal fee |